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WO2018045398A1 - Catalyseur zsm-5 dopé au bi-métal - Google Patents

Catalyseur zsm-5 dopé au bi-métal Download PDF

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Publication number
WO2018045398A1
WO2018045398A1 PCT/ZA2017/050049 ZA2017050049W WO2018045398A1 WO 2018045398 A1 WO2018045398 A1 WO 2018045398A1 ZA 2017050049 W ZA2017050049 W ZA 2017050049W WO 2018045398 A1 WO2018045398 A1 WO 2018045398A1
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catalyst
zsm
hzsm
catalysts
samples
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Inventor
Masikana Millan Mdleleni
David Key
Andrii KOSTYNIUK
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Petroleum Oil and Gas Corp of South Africa Pty Ltd
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Petroleum Oil and Gas Corp of South Africa Pty Ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
    • B01J29/48—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing arsenic, antimony, bismuth, vanadium, niobium tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/70—Catalysts, in general, characterised by their form or physical properties characterised by their crystalline properties, e.g. semi-crystalline
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G50/00—Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/10—After treatment, characterised by the effect to be obtained
    • B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
    • B01J2229/186—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself not in framework positions
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2235/00—Indexing scheme associated with group B01J35/00, related to the analysis techniques used to determine the catalysts form or properties
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2235/00—Indexing scheme associated with group B01J35/00, related to the analysis techniques used to determine the catalysts form or properties
    • B01J2235/10—Infrared [IR]
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2235/00—Indexing scheme associated with group B01J35/00, related to the analysis techniques used to determine the catalysts form or properties
    • B01J2235/15—X-ray diffraction
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2235/00—Indexing scheme associated with group B01J35/00, related to the analysis techniques used to determine the catalysts form or properties
    • B01J2235/30—Scanning electron microscopy; Transmission electron microscopy
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/04—Diesel oil

Definitions

  • This invention relates to a Bi-metal doped ZSM-5 Catalyst for the oligomerisation of light olefins.
  • the invention also relates to the oligomerisation of olefins and a method for manufacturing a catalyst.
  • the inventor is aware of the use of metal promoted ZSM-5 catalysts for the heterogeneous oligomerisation of light olefins.
  • HZSM-5 zeolite is one of the best solid acid catalyst and have been widely applied in petrochemical industry, due to their unique structures, thermal stability, acidity and shape selectivity [10, 12, 13].
  • a catalyst for the heterogeneous oligomerisation of a 1 -hexene containing feed stream to produce distillates in the gasoline and/ or diesel range which catalyst includes:
  • HZSM-5 catalyst modified with between 4 and 6 weight percent Fe and Mo in a ratio range of 1 :5 to 5:1 .
  • the catalyst may preferably modified with between 2.4:2.6 and 3.1 :2.9 weight percent Fe and Mo to provide a catalyst with high gasoline selectivity and low Ci to C5 selectivity.
  • Oligomerisation may be carried out at about 350°C for about 6 hours on-stream at atmospheric pressure using a fixed-bed reactor.
  • the reactor may be a quartz tube reactor.
  • the method may include selecting a specific ratio of Fe and Mo to manipulate the selectivity towards gasoline or diesel during oligomerisation.
  • the invention also extends a method to produce distillates in the gasoline and/ or diesel range by contacting a 1 -hexene containing feed stream with a HZSM-5 oligomerisation catalyst modified with between 4 and 6 weight percent Fe and Mo in a ratio range of 1 :5 to 5: 1 .
  • the invention also extends to the use of the heterogeneous oligomerisation catalyst to produce distillates in the gasoline and/ or diesel range as described.
  • the invention also extends to a method for the manufacture of an oligomerisation catalyst, wherein calcined NH 4 -ZSM-5 zeolite (S1O2/AI2O3 ⁇ 30) was impregnated by incipient wetness impregnation method firstly with a solution of ammonium heptamolybdate ( ⁇ 4 )6 ⁇ 7 ⁇ 2 -4 ⁇ 2 ⁇ and secondly with a solution of iron(lll) nitrate Fe(N0 3 ) 3 -9H 2 0.
  • calcined NH 4 -ZSM-5 zeolite S1O2/AI2O3 ⁇ 30
  • Figure 1 shows N2-adsorption and desorption isotherms (a); BJH pore size distribution (b) of the HZSM-5 and xFeyMo-ZSM-5 samples.
  • Figure 2 shows HRSEM images of the HZSM-5 and xFeyMo-ZSM-5 samples with fixed loading and variable Mo/Fe ratio (A - HZSM-5, B - 5Mo, C - 1 Fe4Mo, D - 1.25Fe3.75Mo, E - 1.43Fe3.57Mo, F - 1 .67Fe3.33Mo, G - 2Fe3Mo, H - 2.5Fe2.5Mo, I - 3Fe2Mo, J - 4Fe1 Mo, K - 5Fe).
  • Figure 3 shows Element mapping of the HZSM-5 (A), 5Fe-ZSM-5 (B), 5Mo- ZSM-5 (C), 2.5Fe2.5Mo-ZSM-5 (D).
  • Figure 4 shows HRTEM images of the xFeyMo-ZSM-5 catalysts with fixed loading and variable Mo/Fe ratio (A - HZSM-5, B - 5Mo, C - 1 Fe4Mo, D - 1.25Fe3.75Mo, E - 1.43Fe3.57Mo, F - 1 .67Fe3.33Mo, G - 2Fe3Mo, H - 2.5Fe2.5Mo, I - 3Fe2Mo, J - 4Fe1 Mo, K - 5Fe).
  • Figure 5 shows EDX spectra of HZSM-5 and xFeyMo-ZSM-5 samples.
  • Figure 6 shows FT-IR spectra of the HZSM-5 and xFeyMo-ZSM-5 catalysts.
  • Figure 7 shows XRD patterns of the HZSM-5 and xFeyMo-ZSM-5 catalysts.
  • Figure 8 shows XRD patterns of the HZSM-5 and xFeyMo-ZSM-5 samples.
  • Figure 9 shows the Conversion of 1 -hexene for the experiments with 1.0 g catalyst and time-on-stream of 6 h.
  • Figure 1 1 shows Selectivity C1 -C5, C6-C9, Cg and C10+ hydrocarbons over HZSM-5, 2.5Fe2.5Mo-ZSM-5 and 3Fe2Mo-ZSM-5 samples.
  • H 4 - ZSM-5 zeolite Zeolyst Int., CBV 3024E
  • Iron(III) nitrare Sigma-Aldrich, 98+%)
  • Ammonium molybdate tetrahydrate Sigma-Aldrich, 99.98%)
  • 1-Hexene Sigma-Aldrich
  • the preparation of the xFeyMo-ZSM-5 catalysts was involved the impregnation of a calcined commercial H4-ZSM-5 zeolite (S1O 2 /AI2O3 ⁇ 30) using the incipient wetness impregnation method with solutions of ammonium heptamolybdate ( ⁇ 4 ) 6 ⁇ 7 ⁇ 24 4H 2 0 and iron(III) nitrate Fe(N0 3 ) 3 - 9H 2 0.
  • the NH 4 -ZSM-5 powder was calcined at 550 °C in air for 6 h to convert the powder from the ammonium form to its protonated form.
  • Samples containing both molybdenum and iron were prepared by a two-step impregnation procedure, in which the molybdenum phase was introduced first. Then samples were dried overnight at 120 °C and calcined at 500 °C for 6 hours. Similarly, 5wt%Fe-ZSM-5 and 5wt%Mo-ZSM-5 catalysts were prepared by impregnation method.
  • the FTIR framework spectra were obtained by using Perkin Elmer FTIR spectrometer. The sample were then analysed 400 to 4000 cm "1 at room temperature. The spectral data were collected on the computer equipped copyright 2012 Perkin Elmer, Inc. version 10.03.07.
  • BET surface area was determined using a Micrometrics 3300, TriStar surface area and porosity analyser. About 0.3 g of sample was degassed at 400 °C for 4 hours. After degassing process the samples were then loaded on the analysis station for determination of the isotherms at -196 °C. The pore size distributions were calculated using the Barrett-Joyner- Halenda (BJH) model applied to the desorption branch of the isotherm, assuming cylindrical pore geometry. SEM analysis
  • SEM micrographs were obtained using a high resolution SEM EHT 5.00 kV. All samples were carbon coated before imaging.
  • the HRSEM (AURIGA) was also equipped with an EDS spectrometer with the INCA EDS system by Oxford Instruments for elemental analysis of zeolites.
  • Transmission electron microscopy images were obtained using aid of HRTEM techniques using a FEI Tecnai TF20 (20()kV) equipped with a STEM: unit, high-angle annular dark-field (HAADF) detector and X-Twin lenses.
  • FEI Tecnai TF20 (20()kV) equipped with a STEM: unit, high-angle annular dark-field (HAADF) detector and X-Twin lenses.
  • HAADF high-angle annular dark-field
  • the performances of the zeolite catalysts were tested in the conversion of 1 -hexene in a fixed bed quartz tube reactor at a weight hourly space velocity (WHSV) of 4 h "1 and the reaction temperature was kept at 350 °C under atmospheric pressure.
  • the reactor tube was charged with 1 g of a catalyst then heated from room up to 350 °C.
  • 1 -hexene was introduced by syringe pump at a flow rate of 0.098 ml/min with the syringe of 29 mm diameter continuously for 6 hours.
  • Table 1 summarizes the nominal composition of samples with different Mo/Fe ratio and fixed loading (5 wt%).
  • the BET surface area (SBET), microporous surface area (Smicro), external surface area (S ex trer), microporous volume (V m i cr o), total pore volume (V to tai) and average pore diameters of the studied catalysts are listed in Table 2 [17].
  • the micropore volume of HZSM-5 zeolite was reduced from 0.105 to 0.092 cmVg, as revealed in Table 2.
  • the BET surface area decreased from 377 to 313 cm 2 /g due to strong Mo interaction with HZSM-5 and the high dispersion of Mo into the zeolite channels [17-19].
  • Adding 5wt% Fe to HZSM-5 catalyst has shown in a decrease of SBET, Smicro, S ex trer, Vmicro, V to tai indicating that Fe mostly deposited on the external surfaces and could have blocked some of the micropores of HZSM- 5 [17].
  • the xFeyMo-ZSM-5 samples exhibit a different behavior with variable Mo Fe ratio.
  • the xFeyMo-ZSM-5 samples exhibit a greater surface area than 5wt%Mo-ZSM-5 suggesting a better dispersion when both metals are present [17, 19].
  • Figure. 1 (a) provides the N 2 ad sorption-de sorption isotherms for samples with different Mo Fe ratio.
  • the characteristic of the xFeyMo-ZSM-5 samples tends to agglomerate into microsized agglomerates is also featured by its N 2 adsorption and desorption isotherms, which could also be supported by the results of XRD and SEM results [18] .
  • Figure. 1 (a) provides the N 2 ad sorption-de sorption isotherms for samples with different Mo Fe ratio.
  • the characteristic of the xFeyMo-ZSM-5 samples tends to agglomerate into microsized agglomerates is also featured by its N 2 adsorption and desorption isotherms, which could also be supported by the results of XRD and SEM results [18] .
  • Figure. 1 (a) provides the N 2 ad sorption-de sorption isotherms for samples with different Mo Fe ratio.
  • FIG. 1 (b) shows the meso- and macropores with sizes in a wide range of 3-100 nm [16] . The majority of these pores concentrated at about 12-15 nm. Thus, impregnation does not change the texture of catalysts which agrees with XRD, FTIR, SEM and TEM results [25].
  • FIG. 2 HRSEM images of the HZSM-5 and xFeyMo-ZSM-5 samples with fixed loading and variable Mo/Fe ratio (A - HZSM-5, B - 5Mo, C - lFe4Mo, D - 1.25Fe3.75Mo, E - 1.43Fe3.57Mo, F - 1.67Fe3.33Mo, G - 2Fe3Mo, H - 2.5Fe2.5Mo, I - 3Fe2Mo, J - 4FelMo, K - 5Fe).
  • FIG. 3 Element mapping of the HZSM-5 (A), 5Fe-ZSM-5 (B), 5Mo-ZSM-5 (C), 2.5Fe2.5Mo-ZSM-5 (D).
  • FIG. 4 HRTEM images of the xFeyMo-ZSM-5 catalysts with fixed loading and variable Mo/Fe ratio (A - HZSM-5, B - 5Mo, C - lFe4Mo, D - 1.25Fe3.75Mo, E - 1.43Fe3.57Mo, F - 1.67Fe3.33Mo, G - 2Fe3Mo, H - 2.5Fe2.5Mo, I - 3Fe2Mo, J - 4FelMo, K - 5Fe).
  • the FT-IR spectra of the HZSM-5 and xFeyMo-ZSM-5 samples were recorded in the range of 400-4000 cm and shown in Figure. 6.
  • the absorption bands at 1220, 1075, 797, 542, 433 cm “1 are considered as the characteristic signals for the framework vibration of the HZSM-5 zeolite catalyst [29]. It was found that the band 433 cm “1 belongs to the T-0 bending vibration of internal tetrahedral, 542 cm “1 (double ring), 797 cm “1 (external symmetric stretch), 1075 cm “1 (internal asymmetric stretch) and 1220 cm “1 (external asymmetric stretch), respectively [25,29-31].
  • FIG. 6 FT-IR spectra of the HZSM-5 and xFeyMo-ZSM-5 catalysts.
  • the spectrum of xFeyMo-ZSM-5 catalyst shows major changes in the region of 750-1000 cm “1 , weakening of strong absorption of band at 797 cm “1 . It was found new broad at 901 cm “1 , which corresponds to the overlap between Mo-O-Mo bond vibrations and Mo-O-Fe bond vibrations in Fe2(MoC>4)3.
  • the band at 1075 cm “1 is sensitive to the ratio of framework Si/Al. By the loading of FeMo species, the band at 1075 cm “1 shifted to 1081 cm “1 ( Figures. 6).
  • Figures. 10-11 show that addition of Fe-Mo to HZSM-5 led to decrease in the selectivity of C1-C5 fragments.
  • An average selectivity of between 23-37% was obtained for the 2.5wt%Fe2.5wt%Mo-ZSM-5 and 3wt%Fe2wt%Mo-ZSM-5 zeolite catalysts.
  • the average selectivity for the parent FIZSM-5 was between 27-43%.
  • Figure. 12 shows the product distribution of grouped fractions of C 1-C17+ from the liquid product for 2.5wt%Fe2.5wt%Mo-ZSM-5, 3wt%Fe2wt%Mo-ZSM-5 and HZSM-5.
  • the product distribution of C 8 , C9 and C 10 were 15%, 19% and 14% respectively for the HZSM-5 catalyst.
  • the product distribution of C 8 , C9, C 10 and Cn increase to 33%, 33%, 23% and 15% respectively for the 2.5wt%Fe2.5wt%Mo-ZSM-5 and 3wt%Fe2wt%Mo-ZSM-5. Summary
  • aluminosilicate zeolites, MCM-41, and silica-alumina co-gel catalysts A comparative study. J Catal 1999;184:262-7. doi: 10.1006/jcat. l999.2423.
  • Fischer- Tropsch type feed materials Energy and Fuels 2007;21 :3084-9.
  • Mo/ZSM-5 synthesized by solid state reaction for methane dehydrogenation and aromatization. Microporous Mesoporous Mater 2006;88:244-53.
  • nanocrystalline ZSM-5 zeolite Catal Today 2012; 195 :59-70.

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Abstract

L'invention concerne un catalyseur et un procédé pour l'oligomérisation hétérogène d'un flux d'alimentation contenant du 1-hexène en vue de produire des distillats dans la gamme de l'essence et/ou du gasoil. Le catalyseur comprend un catalyseur HZSM-5 modifié comportant entre 4 et 6 pour cent en poids de Fe et de Mo dans une plage de rapport allant de 1:5 à 5:1. Le catalyseur peut de préférence être modifié avec entre 2,4:2,6 et 3,1:2,9 pour cent en poids de Fe et de Mo pour fournir un catalyseur ayant une sélectivité élevée envers l'essence et une faible sélectivité envers les C1 à C5.
PCT/ZA2017/050049 2016-09-01 2017-08-28 Catalyseur zsm-5 dopé au bi-métal Ceased WO2018045398A1 (fr)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN116477640A (zh) * 2023-05-16 2023-07-25 中国矿业大学 一种固相法直接制备磷改性h型zsm-5分子筛的方法
CN119565624A (zh) * 2024-12-03 2025-03-07 大连理工大学 一种用于scr烟气脱硝的新型催化剂、其制备方法与应用

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WO2016123640A2 (fr) * 2015-01-29 2016-08-04 The Petroleum Oil And Gas Corporation Of South Africa (Pty) Ltd Catalyseur d'oligomérisation

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WO2016123640A2 (fr) * 2015-01-29 2016-08-04 The Petroleum Oil And Gas Corporation Of South Africa (Pty) Ltd Catalyseur d'oligomérisation

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